US4491924A - Olefin oxidation reactor temperature control - Google Patents

Olefin oxidation reactor temperature control Download PDF

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Publication number
US4491924A
US4491924A US06/375,795 US37579582A US4491924A US 4491924 A US4491924 A US 4491924A US 37579582 A US37579582 A US 37579582A US 4491924 A US4491924 A US 4491924A
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United States
Prior art keywords
reactor
temperature
effluent
product
coolant
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Expired - Fee Related
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US06/375,795
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English (en)
Inventor
Suresh C. Agarwal
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Elsag International BV
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Babcock and Wilcox Co
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Publication date
Priority claimed from US06/370,703 external-priority patent/US4488239A/en
Assigned to BABCOCK & WILCOX COMPANY, THE reassignment BABCOCK & WILCOX COMPANY, THE ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: AGARWAL SURESH C
Priority to US06/375,795 priority Critical patent/US4491924A/en
Application filed by Babcock and Wilcox Co filed Critical Babcock and Wilcox Co
Priority to ES522344A priority patent/ES8404528A1/es
Priority to IN546/CAL/83A priority patent/IN160808B/en
Priority to EP83302539A priority patent/EP0094208B1/en
Priority to DE8383302539T priority patent/DE3374841D1/de
Priority to AU14305/83A priority patent/AU559836B2/en
Priority to JP58078397A priority patent/JPS6033537B2/ja
Priority to CA000427648A priority patent/CA1187267A/en
Priority to BR8302460A priority patent/BR8302460A/pt
Publication of US4491924A publication Critical patent/US4491924A/en
Application granted granted Critical
Assigned to BABCOCK & WILCOX TRACY POWER, INC., A CORP. OF DE reassignment BABCOCK & WILCOX TRACY POWER, INC., A CORP. OF DE ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: BABCOCK & WILCOX COMPANY, THE, A CORP. OF DE
Assigned to ELSAG INTERNATIONAL B.V., A CORP. OF THE NETHERLANDS reassignment ELSAG INTERNATIONAL B.V., A CORP. OF THE NETHERLANDS ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: BABCOCK & WILCOX TRACY POWER, INC., A CORP. OF DE
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/001—Controlling catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D301/00—Preparation of oxiranes
    • C07D301/02—Synthesis of the oxirane ring
    • C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
    • C07D301/04—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen
    • C07D301/08—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00088—Flow rate measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00097—Mathematical modelling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00054—Controlling or regulating the heat exchange system
    • B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2219/00058—Temperature measurement
    • B01J2219/0006—Temperature measurement of the heat exchange medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00054—Controlling or regulating the heat exchange system
    • B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2219/00069—Flow rate measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00085—Plates; Jackets; Cylinders
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock

Definitions

  • the present invention relates, in general, to temperature controlled equipment techniques in chemical reactors and, in particular, to a new and useful temperature control system for an olefin oxidation reactor which regulates the rate of coolant flow to maintain the reactor temperature within a desired temperature range, during the operation of the reactor as well as during start-up, shut-down and transient operating conditions.
  • U.S. Pat. No. 3,471,582 to Lupfer discloses an arrangement wherein a desired temperature across an exothermic reactor is maintained by controlling the reactor feed temperature in response to a difference in the temperature between the reactant feed and product stream from the reactor until a maximum predetermined product temperature is obtained.
  • U.S. Pat. No. 3,271,472 to Ogle et al discloses apparatus for controlling the operation of a thermal cracking furnace. Since the thermal cracking of hydrocarbons is an endothermic reaction, it is necessary to maintain a maximum possible temperature within the equipment limits. A minimum temperature is not considered or important in Ogle et al.
  • ethylene and oxygen or air is mixed and fet to an isothermal multitubular reactor.
  • Ethylene is oxidized into ethylene oxide in the presence of a catalyst and carbon dioxide and water are produced as by-products.
  • Reactor temperature control objectives are:
  • Reactor temperature control is of key significance because of the following factors:
  • the most economical temperature for oxidation is one at which the highest conversion to ethylene oxide occurs rather than to by-products.
  • Increase in reaction temperature produces two effects: (1) overall rate of ethylene oxidation increases, and (2) catalyst selectivity to ethylene oxide decreases such that relatively more ethylene is converted into carbon dioxide and water. Moreover, heat generation increases by the fact that more ethylene is oxidized and overall reaction becomes less selective. Consequently, increase in temperature may result in:
  • reactor temperature control system is based on manipulating coolant flow rate. Its set point is directly based upon average reactor temperature.
  • An object of the present invention is to provide a control system and techniques which accomplishes the objectives of operating an olefin oxidation reactor at the most economical and safe temperature range, with regard to a maximum conversion of the olefin to the desired olefin oxide and a minimization of by-products.
  • Another object of the invention is to provide such a control system and technique, in particular for ethylene oxidation reactors.
  • Another object of the invention is to provide a control system and technique which is also applicable to other exothermic and endothermic reactors.
  • a system which controls the rate of coolant flow in the chemical reactor according to an algorithm which incorporates various parameters including reactor feed and effluent flow rates, specific heat of reactants and products, reactor and effluent temperatures, coolant heat of evaporation, reactant and product concentration and heat of reactions for various reactions taking place in the reactor.
  • temperatures are taken at varied locations along the reactor length, for obtaining a maximum and a minimum value for temperatures within the reactor for establishing a desired reactor temperature range.
  • Another objective of the invention is to provide a temperature control system and method for an olefin oxidation reactor which is simple in design, rugged in construction and economical to manufacture.
  • Another important feature of the invention is to provide an arrangement as set forth above for controlling the rate of coolant flow which, additionally, compensates for variations in operating conditions as well as provides proper coolant flow control even during start-up and shutdown phases of the operation.
  • FIG. 1 is a schematic representation of the inventive control system in combination with a tubular reactor for containing an olefin oxidation reaction;
  • FIG. 2 is a block diagram which illustrates an exemplary computer layout for achieving the inventive purpose.
  • the invention embodied therein in FIG. 1 comprises a control arrangement for controlling the flow of coolant into a tube reactor 10 by controlling the position of a valve 100 in a coolant inlet line.
  • Controller valve 100 is achieved over line 112 connected to the output of a computer 20 which receives various inputs carrying signals corresponding to temperatures at various locations in the reactor and in the reactor feed and effluent lines and component concentrations.
  • the computer is programmed with constants which relate to heats of various reactions going on in the reactor 10 and various physical characteristics of the coolant, the reactants and the products of the reaction.
  • coolant flow rate is given by the expression ##EQU1## where:
  • T I Feed inlet temperature
  • T O Reactor Exit Stream temperature
  • ⁇ H 1 Heat of reaction for oxidation to ethylene oxide
  • ⁇ H 2 Heat of reaction for oxidation to carbon dioxide and water
  • y 1 a first produce (ethylene oxide) concentration
  • y 2 a second produce (CO 2 ) concentration.
  • equation (1) can be written as
  • a control system according to the invention can thus be obtained where all measured signals are interfaced to a control computer system by state of the art methods.
  • a total control system is shown in Fig. 1.
  • the outputs are: coolant flow control valve setting at 112; minimum and maximum temperature signals to start-up and shut-down control systems (not shown here), and to display units at 114; and high low temperature alarms at 116.
  • Other measured signals can be checked for high and/or low limits and alarmed as per need and operating practices of an individual reactor system.
  • control computer system While the implementation shown herein is through a control computer system, the invention can also be easily implemented by conventional electronic instrumentation and control systems.
  • a plurality of temperature transmitters 62 provide temperature signals to computer 20 for the reactor feed line, the reactor 10 at various longitudinal locations thereof and the reactor effluent line.
  • Each of the analog signals is converted in a corresponding analog to digital converter 63 into a corresponding digital signal which is readable by computer 20.
  • the invention is provided with a plurality of flow transmitters 44 and a plurality of concentration transmitters 50.
  • Flow transmitters 44 provide analog signals which similarly are converted to corresponding digital signals corresponding to the reactor feed and effluent flow rate as well as the coolant flow rate.
  • Concentration transmitters 50 provide signals corresponding to the concentration of various components in the feed and effluent line.
  • Temperature transmitters TT-11 through TT-1M provide their signals to a signal processing block B-2.
  • the signals are then processed in a block B-4 to determine the maximum and minimum temperatures along the longitudinal length of the reactor.
  • the signal is then supplied over line 14 to an output of computer 20 and also to a block B-9 for achieving calculations as pointed out above.
  • Limit checking is accomplished in a block B-5 for sounding a low or high temperature alarm over line 116.
  • Equation (4) is utilized with each differential factor calculated as shown in equations (5) to equation (11).
  • Simple comparators which relate an initial value with a later value can be utilized in computer 20 to obtain the values of flow rate change, ⁇ F 1 and ⁇ F 2 , as well as the temperature and concentration change.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Control Of Temperature (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US06/375,795 1982-04-22 1982-05-07 Olefin oxidation reactor temperature control Expired - Fee Related US4491924A (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US06/375,795 US4491924A (en) 1982-04-22 1982-05-07 Olefin oxidation reactor temperature control
ES522344A ES8404528A1 (es) 1982-05-07 1983-04-29 Sistema de control de temperatura en un reactor de oxidacion de olefina.
IN546/CAL/83A IN160808B (ja) 1982-05-07 1983-05-04
DE8383302539T DE3374841D1 (en) 1982-05-07 1983-05-05 Reactor temperature control systems
EP83302539A EP0094208B1 (en) 1982-05-07 1983-05-05 Reactor temperature control systems
AU14305/83A AU559836B2 (en) 1982-05-07 1983-05-06 Chemical reactor temperature control
JP58078397A JPS6033537B2 (ja) 1982-05-07 1983-05-06 オレフイン酸化反応器温度制御装置
CA000427648A CA1187267A (en) 1982-05-07 1983-05-06 Olefin oxidation reactor temperature control
BR8302460A BR8302460A (pt) 1982-05-07 1983-05-09 Controle de temperatura de reator para oxidacao de olefinas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US06/370,703 US4488239A (en) 1982-04-22 1982-04-22 Temperature control system for olefin oxidation reactor
US06/375,795 US4491924A (en) 1982-04-22 1982-05-07 Olefin oxidation reactor temperature control

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
US06/370,703 Continuation-In-Part US4488239A (en) 1982-04-22 1982-04-22 Temperature control system for olefin oxidation reactor

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US4491924A true US4491924A (en) 1985-01-01

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US06/375,795 Expired - Fee Related US4491924A (en) 1982-04-22 1982-05-07 Olefin oxidation reactor temperature control

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US (1) US4491924A (ja)
EP (1) EP0094208B1 (ja)
JP (1) JPS6033537B2 (ja)
AU (1) AU559836B2 (ja)
BR (1) BR8302460A (ja)
CA (1) CA1187267A (ja)
DE (1) DE3374841D1 (ja)
ES (1) ES8404528A1 (ja)
IN (1) IN160808B (ja)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4654801A (en) * 1984-11-30 1987-03-31 Phillips Petroleum Company Control of a vinyl acetate process
US4668473A (en) * 1983-04-25 1987-05-26 The Babcock & Wilcox Company Control system for ethylene polymerization reactor
DE3643136A1 (de) * 1985-12-27 1987-07-02 Mitsui Toatsu Chemicals Verfahren zur steuerung der polymerisationstemperatur
US4707245A (en) * 1985-12-20 1987-11-17 Lummus Crest, Inc. Temperature control for hydrogenation reactions
US4742472A (en) * 1984-05-24 1988-05-03 Mitsubishi Rayon Co., Ltd. Method and apparatus for controlling polymerization reaction
US4858155A (en) * 1985-12-24 1989-08-15 Beckman Instruments, Inc. Reaction temperature control system
US4881185A (en) * 1986-04-01 1989-11-14 Chugai Ro. Co., Ltd. Method of measuring temperature and apparatus for effecting the method
US4888704A (en) * 1987-12-18 1989-12-19 Amoco Corporation Advanced control strategies for melt flow rate and reactor concentration in the polypropylene slurry process
US5000924A (en) * 1987-06-02 1991-03-19 Elsagainternational B.V. Autoacceleration control for exothermic reactors
AU608002B2 (en) * 1987-06-02 1991-03-21 International Control Automation Finance Sa Autoacceleration control for exothermic reactors
US6284196B1 (en) * 1999-04-01 2001-09-04 Bp Corporation North America Inc. Apparatus for monitor and control of an ammoxidation reactor with a fourier transform infrared spectrometer
US20020001547A1 (en) * 2000-04-26 2002-01-03 Michael Raymond Connelly Polymer process
US6590131B2 (en) * 2000-04-27 2003-07-08 Bp Corporation North America Inc. Method for control of a chemical manufacturing process
US20050002831A1 (en) * 2001-08-31 2005-01-06 Robert Ashe Multi-port flow control valves
US20070287819A1 (en) * 2006-06-13 2007-12-13 Sumitomo Chemical Company, Limited Method for measuring concentration of propylene polymer slurry, and process for producing propylene polymer
US11111446B2 (en) * 2015-11-18 2021-09-07 Catech Technology Co., Ltd. Temperature-controlling measure for the hydrogenation slurry bed reactor and its design method and use

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US4958826A (en) * 1988-08-08 1990-09-25 Microtek Lab., Inc. Paper feed system having a pressure plate that resiliently urges a plurality of elongated bearing, spring biased idler rollers against associated drive rollers for feeding a sheet of paper therebetween
NO178790C (no) * 1993-12-13 1996-06-05 Borealis Holding As Fremgangsmåte ved fremstilling av olefinpolymerer i en autoklavrektor
EP1447128A1 (en) 2003-02-17 2004-08-18 Methanol Casale S.A. Method for carrying out chemical reactions in pseudo-isothermal conditions
WO2008058918A1 (de) * 2006-11-15 2008-05-22 Basf Se Verfahren zum betreiben einer exothermen heterogen katalysierten partiellen gasphasenoxidation einer organischen ausgangsverbindung zu einer organischen zielverbindung
CN112973580B (zh) * 2021-02-08 2022-01-21 湖北昌发容器制造有限公司 一种耐酸耐高温的无汞触媒催化氯乙烯转化器

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US4111218A (en) * 1974-05-30 1978-09-05 Phillips Petroleum Company Absorption process method and apparatus
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US4236219A (en) * 1979-05-02 1980-11-25 Phillips Petroleum Company Temperature control of exothermic reactions
US4241230A (en) * 1979-11-19 1980-12-23 Mobil Oil Corporation Control system for the selective hydrogenation of acetylene present in ethylene product streams
US4249907A (en) * 1979-08-23 1981-02-10 Phillips Petroleum Company Temperature control of exothermic reactions
US4249908A (en) * 1979-09-11 1981-02-10 Phillips Petroleum Company Temperature control of exothermic reactions
US4329150A (en) * 1980-12-11 1982-05-11 Mobil Oil Corporation Method and apparatus for control and optimization of pyrolysis furnace with multiple parallel passes

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Publication number Priority date Publication date Assignee Title
US3271472A (en) * 1961-09-22 1966-09-06 Phillips Petroleum Co Method of controlling a thermal conversion process
US3471582A (en) * 1967-11-16 1969-10-07 Phillips Petroleum Co Control of exothermic reactions
US4111218A (en) * 1974-05-30 1978-09-05 Phillips Petroleum Company Absorption process method and apparatus
US4132530A (en) * 1977-10-13 1979-01-02 Uop Inc. Temperature control in exothermic/endothermic reaction systems
US4236219A (en) * 1979-05-02 1980-11-25 Phillips Petroleum Company Temperature control of exothermic reactions
US4249907A (en) * 1979-08-23 1981-02-10 Phillips Petroleum Company Temperature control of exothermic reactions
US4249908A (en) * 1979-09-11 1981-02-10 Phillips Petroleum Company Temperature control of exothermic reactions
US4241230A (en) * 1979-11-19 1980-12-23 Mobil Oil Corporation Control system for the selective hydrogenation of acetylene present in ethylene product streams
US4329150A (en) * 1980-12-11 1982-05-11 Mobil Oil Corporation Method and apparatus for control and optimization of pyrolysis furnace with multiple parallel passes

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4668473A (en) * 1983-04-25 1987-05-26 The Babcock & Wilcox Company Control system for ethylene polymerization reactor
US4742472A (en) * 1984-05-24 1988-05-03 Mitsubishi Rayon Co., Ltd. Method and apparatus for controlling polymerization reaction
US4654801A (en) * 1984-11-30 1987-03-31 Phillips Petroleum Company Control of a vinyl acetate process
US4707245A (en) * 1985-12-20 1987-11-17 Lummus Crest, Inc. Temperature control for hydrogenation reactions
US4858155A (en) * 1985-12-24 1989-08-15 Beckman Instruments, Inc. Reaction temperature control system
DE3643136A1 (de) * 1985-12-27 1987-07-02 Mitsui Toatsu Chemicals Verfahren zur steuerung der polymerisationstemperatur
US4881185A (en) * 1986-04-01 1989-11-14 Chugai Ro. Co., Ltd. Method of measuring temperature and apparatus for effecting the method
US5000924A (en) * 1987-06-02 1991-03-19 Elsagainternational B.V. Autoacceleration control for exothermic reactors
AU608002B2 (en) * 1987-06-02 1991-03-21 International Control Automation Finance Sa Autoacceleration control for exothermic reactors
US4888704A (en) * 1987-12-18 1989-12-19 Amoco Corporation Advanced control strategies for melt flow rate and reactor concentration in the polypropylene slurry process
US6284196B1 (en) * 1999-04-01 2001-09-04 Bp Corporation North America Inc. Apparatus for monitor and control of an ammoxidation reactor with a fourier transform infrared spectrometer
US20020001547A1 (en) * 2000-04-26 2002-01-03 Michael Raymond Connelly Polymer process
US6991763B2 (en) 2000-04-26 2006-01-31 Rohm And Haas Company Polymer process
US6590131B2 (en) * 2000-04-27 2003-07-08 Bp Corporation North America Inc. Method for control of a chemical manufacturing process
US20050002831A1 (en) * 2001-08-31 2005-01-06 Robert Ashe Multi-port flow control valves
US7736604B2 (en) * 2001-08-31 2010-06-15 Ashe Morris Ltd Multi-port flow control valves
US20070287819A1 (en) * 2006-06-13 2007-12-13 Sumitomo Chemical Company, Limited Method for measuring concentration of propylene polymer slurry, and process for producing propylene polymer
US11111446B2 (en) * 2015-11-18 2021-09-07 Catech Technology Co., Ltd. Temperature-controlling measure for the hydrogenation slurry bed reactor and its design method and use

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CA1187267A (en) 1985-05-21
IN160808B (ja) 1987-08-08
ES522344A0 (es) 1984-04-16
EP0094208B1 (en) 1987-12-09
EP0094208A2 (en) 1983-11-16
ES8404528A1 (es) 1984-04-16
AU1430583A (en) 1984-11-08
JPS5925382A (ja) 1984-02-09
EP0094208A3 (en) 1985-07-10
JPS6033537B2 (ja) 1985-08-03
BR8302460A (pt) 1984-01-17
AU559836B2 (en) 1987-03-19
DE3374841D1 (en) 1988-01-21

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